atv-dvwk_a_131_e

(1)

GERMAN ATV-DVWK

RULES AND STANDARDS

STANDARD

ATV-DVWK-A 131E

Dimensioning of Single-Stage Activated Sludge Plants

May 2000

ISBN 3-935669-96-8

Distribution: GFA Publishing Company of ATV-DVWK Water, Wastewater and Waste Theodor-Heuß-Allee 17 • D-53773 Hennef • Postfach 11 65 • D-53758 Hennef Telephone: +49-2242/872-120 • Telefax: +49-2242/872-100

(2)

Preparation

This ATV Standard has been elaborated by the ATV-DVWK Specialist Committees KA 5 and KA 6.

Specialist Committee KA 5 “Settling Processes” has the following members Prof. Dr.-Ing. Günthert, München (Chairman)

Prof. Dr.-Ing. Billmeier, Köln Dipl.-Ing. Born, Kassel

Dr.-Ing. Andrea Deininger, Weyarn Dr.-Ing. Grünebaum, Essen

Dr.-Ing. Kalbskopf, Dinslaken

Dr.-Ing, Resch, Weissenburg

Prof. Dr.-Ing. Rosenwinkel, Hannover Dr.-Ing. Rölle Stuttgart

Dr.-Ing. Schulz, Essen

Prof. Dr.-Ing. Seyfried, Hannover Dr.-Ing. Stein, Emsdetten

Specialist Committee KA 6 “Aerobic Biological Wastewater Treatment Processes“ has the following members

Prof. Dr.-Ing. Kayser, Braunschweig (Chairman) Dipl.-Ing. Beer, Cottbus

Dr.-Ing. Bever, Oberhausen Prof. Dr.-Ing. Bode, Essen Dr.-Ing. Boll, Hannover Prof. Dr.-Ing. Gujer, Zürich

Prof. Dr. rer. nat. Huber, München Prof. Dr.-Ing. E.h. Imhoff, Essen Prof. Dr.-Ing. Krauth, Stuttgart

Dr. Lemke, Leverkusen Dr. Hilde Lemmer, München Prof. Dr.-Ing. Londong, Wuppertal Prof. Dr. Matsché, Wien

Dipl.-Ing. Peter-Fröhlich, Berlin Prof. Dr.-Ing. Rosenwinkel, Hannover Dipl.-Ing. Schleypen, München Dr.-Ing. Teichgräber, Essen Dipl.-Ing. Ziess, Haan-Gruiten

Die Deutsche Bibliothek [The German Library] - CIP-Einheitsaufnahme ATV-DVWK Standard

A 131E. Dimensioning of Single-Stage Activated Sludge Plants. – 2000 ISBN 3-935669-96-8

All rights, in particular those of translation into other languages, are reserved. No part of this Standard may be reproduced in any form - by photocopy, microfilm or any other process - or transferred into a language usable in machines, in particular data processing machines, without the written approval of the publisher.

 GFA-Gesellschaft zur Förderung der Abwassertechnik e.V

(Publishing Company of ATV-DVWK, Water, Wastewater, Waste), Hennef 2000) Original German edition produced by:DCM, Meckenheim

(3)

Notes for Users

This ATV-DVGW Standard is the result of honorary, technical-scientific/economic collaboration which has been achieved in accordance with the principles applicable therefore (statutes, rules of procedure of the ATV and ATV Standard ATV-A 400). For this, according to precedents, there exists an actual presumption that it is textually and technically correct and also generally recognised.

The application of this Standard is open to everyone. However, an obligation for application can arise from legal or administrative regulations, a contract or other legal reason.

This Standard is an important, however, not the sole source of information for correct solutions. With its application no one avoids responsibility for his own action or for the correct application in specific cases; this applies in particular for the correct handling of the margins described in the Standard.

Foreword

At the time of elaborating the previous issue of this ATV Standard (1988-90) there were only isolated activated sludge plants with nitrogen and phosphorus removal, from whose operating results information could be deduced for dimensioning and operation. Therefore, with many questions, one had to rely exclusively on the results of research. In the meantime, a large number of such facilities have been commissioned so that a wider database, also from practice, is available for a revision.

Compared with the issue of ATV Standard ATV-A 131 dated February 1991 the following important changes have been made:

•

validity for activated sludge plants of any size (up to now ≥ 5,000 total number of inhabitants and population equivalents PT).

•

the chapter on derivation of design flows and loads is taken out, since a separate ATV Standard is to be elaborated for all types of wastewater treatment processes.

•

dimensioning temperature for nitrogen removal T = 12° C in accord with the requirements from Appendix 1 of The [German] Wastewater Ordinance (AbwV) (previously T = 10° C), under the assumption of a flexible design of the biological rector.

•

integration of dimensioning for excess biological phosphorus removal.

•

modification of the denitrification capacity.

•

change of the determination of the required oxygen transfer.

•

integration of the dimensioning of an aerobic selector.

•

option for dimensioning on the basis of the chemical oxygen demand (COD).

•

increase of the permitted sludge volume loading rate of secondary settling tanks.

•

modification of the designation of partial depths and the determination of the depth of the thickening and sludge removal zone of secondary settling tanks.

•

integration of the dimensioning of the sludge removal systems (scrapers) in secondary settling tanks.

Explanations on process technology are to be taken from the ATV Manuals “Biological and advanced wastewater treatment “[1] and “Mechanical wastewater treatment” [2]. The figures additionally mentioned in the text refer to the chapters of the manuals.

(6)

1 Area

of

Application

1.1 Preamble

The treatment of the stormwater in the sewer network and of wastewater in the wastewater treatment plant form one unit for the protection of surface waters. For the dimensioning of the wastewater treatment plant and the stormwater overflows the planning periods are to be matched to each other. The planning period should comprise not more than 25 years.

1.2 Objective

Using the dimensioning values recommended in this standard, for municipal wastewater one can, with single-stage activated sludge plants, meet the achievable minimum effluent requirements which correspond with or undercut the requirements of the [German] Wastewater Ordinance (AbwV) dated 02.09.99, Appendix 1, and the associated sampling regulations. If commercial or industrial wastewater with high fractions of slowly biodegradable and/or inert organic substances is discharged, a higher residual COD than with domestic wastewater can arise. The same applies for areas with low water consumption and a low infiltration rate, as then the inert COD concentration increases.

Technical regulations are drawn up for the selection of the most practical procedure for carbon, nitrogen and phosphorus removal, and for the dimensioning of the essential components and facilities of the plant. The selection and dimensioning of aeration equipment is not dealt with in this standard.

Since this standard is also applied outside Germany and because locally even stricter requirements can be set, it is not aimed exclusively at the observance of the effluent requirements laid down in Appendix 1 of the Wastewater Ordinance (AbwV).

In accord with the requirements under water law, the structural and operating requirements and the sensitivity of the surface waters the planning through parallel units, reserve equipment etc. is to be oriented towards an appropriately high operational safety.

A prerequisite for the secure function of the plant, planned in accordance with this standard, is that sufficiently qualified, trained and permanently technically supported operating personnel are employed and involved in the planning process, comp. ATV Advisory Leaflet ATV-M 271 „Personalbedarf für den Betrieb kommunaler Kläranlagen“ [Personnel requirement for the operation of municipal sewage treatment plants].

1.3 Scope

This standard basically applies for the dimensioning of single-stage activated sludge plants. Due to the peculiarities of smaller sewage treatment plants attention is drawn to ATV Standards ATV-A 122E and ATV-ATV-ATV-A 126E as well as DIN 4261.

The standard applies for wastewater which essentially originates from households or from plants which serve commercial or agricultural purposes, insofar as the harmfulness of this wastewater can be reduced by means of biological processes with the same success as with wastewater from households.

(7)

2 Symbols

AST m2 Surface area of secondary settling tanks

a - Number of scraper blades in circular settling tanks

Bd,BOD kg/d Daily BOD5 load

Bd,XXX kg/d Daily load for another parameter

BR,BOD kg/(m3 · d) BOD5 volume loading rate

BR,XXX kg/(m3 · d) Volume loading rate with another parameter

BSS,BOD kg/(kg · d) BOD5 sludge loading rate

BSS,XXX kg/(kg · d) Sludge loading rate with another parameter

b d-1_Decay_coefficient

CS mg/l Dissolved oxygen saturation concentration dependent on the

temperature and partial pressure

CX mg/l Dissolved oxygen concentration in aeration tanks (DO)

DST m Diameter of secondary settling tanks

DSV l/m3 _{Diluted sludge volume, 30 minutes settled (to be determined, if}

SV30 is higher than 250 L/m3, what generally is the case)

FT - Temperature factor for endogenous respiration

fC - Peak factor for carbon respiration

fN - Peak factor for ammonium oxidation

fSR - Sludge removal factor, dependent on the type of sludge scraper

h1 m Depth of the clear water zone in secondary settling tanks

h2 m Depth of the separation zone / return flow zone in secondary

settling tanks

h3 m Depth of the density flow and storage zone in secondary settling

tanks

h4 m Depth of the sludge thickening and removal zone in secondary

settling tanks

hIn m Depth of the centre of the inlet aperture (below water surface) of

secondary settling tanks

hSR m Height of a scraper blade or a scraper beam

htot m Total water depth in the secondary settling tank

LFS m Length of a flight scraper in a rectangular tank (LFS ∼ LST)

LRW m Length of the runway of a scraper bridge in rectangular settling

tanks (LRW ∼ LST)

LSL m Length of the sludge layer moved by a scraper blade in a

rectangular settling tank (LSL ~ 15·hSR)

LSR m Scraper blade or scraper beam length in rectangular secondary

settling tanks (LSR ≈ WST)

(8)

MSS,AT kg Mass of suspended solids in the biological reactor / aeration

tank

OC kg/h Oxygen transfer of an aeration facility in clean water with Cx = 0,

T = 20° C and air pressure p = 1013 hPa

αOC kg/h Oxygen transfer of an aeration facility in activated sludge with Cx

= 0, T = 20° C and air pressure p = 1013 hPa OUC,BOD kg/kg Oxygen uptake for carbon removal, referred to BOD5

OUd,C kg/d Daily oxygen uptake for carbon removal

OUd,D kg/d Daily oxygen uptake for carbon removal which is covered by

denitrification

OUd,N kg/d Daily oxygen uptake for nitrification

OUh kg/h Oxygen uptake rate (hourly)

PTXXX I Total number of inhabitants and population equivalents referred

to the parameters XXX, e.g. BOD5, COD etc.

Q m3_/h _{Inflow rate, flow rate, throughflow rate}

QDW,d m3/d Daily wastewater inflow with dry weather

QDW,h m3/h Hourly dry weather flow rate as 2 hr mean

QWW,h m3/h Dimensioning peak flow rate with wet weather from combined

and separate sewer systems QRS m3/h Return (activated) sludge flow rate

QIR m3/h Internal recirculation flow rate at pre-anoxic zone denitrification

process

QRC m3/h Total recirculation flow rate (QRS + QIR) at pre-anoxic zone

denitrification process

QShort m3/h Short circuit sludge flow rate in secondary settling tanks

QSR m3/h Sludge removal flow rate

QWS,d m3/d Daily waste (activated) sludge flow rate

qA m/h Surface overflow rate of secondary settling tanks

qSV l/(m2 · d) Sludge volume surface loading rate of secondary settling tanks

RC - Total recirculation ratio at pre-anoxic zone denitrification process (RC = QRC/Qh,DW)

RS - Return sludge ratio (RS = QRS/Qh,DW or QRS/Qh,WW)

SF - Safety factor for nitrification

SPd kg/d Daily waste activated sludge production (solids)

SPd,C kg/d Daily sludge production from carbon removal

SPd,P kg/d Daily sludge production from phosphorus removal

SSC,BOD5 kg/kg Sludge production from carbon removal referred to BOD5

SSAT kg/m3 Suspended solids concentration in the biological reactor /

aeration tank (MLSS)

SSAT,Step kg/m3 Average suspended solids concentration in the biological

reactor with step-feed denitrification (SSAT,Step > SSEAT)

SSBS kg/m3 Suspended solids concentration in the bottom sludge of

(9)

SSEAT kg/m3 Suspended solids concentration in the effluent of the biological

reactor / aeration tank (usually SSEAT = SSAT)

SSRS kg/m3 Suspended solids concentration of the return (activated) sludge

SSWS kg/m3 Suspended solids concentration of the waste (activated) sludge

SVI l/kg Sludge volume index

T °C Temperature in the biological reactor / aeration tank TER °C Temperature in the biological reactor at which the effluent

requirements for nitrogen have to be met

TDim °C Temperature in the biological reactor / aeration tank upon which

dimensioning is based

TW °C Temperature in the biological reactor in winter, TW < TDim

tD h,d Duration of denitrification phase with intermittent process

tN h,d Duration of the nitrification phase with intermittent process

tR h,d Retention period (e.g. tR = VAT : Qh,DW)

ts h Time for raising and lowering the scraper blade

tSR h Sludge removal interval (Period of time for one loop of a

scraper)

tSS d Sludge age referred to VAT

tSS,dim d Sludge age upon which dimensioning is based

tSS,aerob d Aerobic sludge age referred to VN

tSS,aerob,dim d Aerobic sludge age upon which dimensioning for nitrification is

based

tT h Cycle time with intermittent process (tT = tD + tN)

tTh h Thickening time of the sludge in the secondary settling tank

VAT m3 Volume of the biological reactor / aeration tank

VBioP m3 Volume of an anaerobic mixing tank for biological phosphorus

removal

VD m3 Volume of the biological reactor used for denitrification

VN m3 Volume of the biological reactor used for nitrification

V

Sel

m

3

Volume of an aerobic selector

V

ST

m

3

Volume of the secondary settling tank

v

ret

m/h

Return velocity of the scraper bridge

v

SR

m/h

Scraper bridge velocity (with circular tanks at the

periphery)

WST m Width of rectangular secondary settling tanks

Y mg/mg Yield factor (mg formed biomass (COD) per mg biodegradable COD)

α - Quotient of oxygen transfer in activated sludge and in clean water

(10)

Chemical parameters and concentrations:

CXXX mg/l Concentration of the parameter XXX in the homogenised

sample

SXXX mg/l Concentration of the parameter XXX in the filtered sample (0.45

µm membrane filter)

XXXX mg/l Concentration of the filter residue (solids), XXXX = CXXX - SXXX

Frequently used parameters:

CBOD mg/l Concentration of BOD5 in the homogenised sample

CCOD mg/l Concentration of COD in the homogenised sample

CCOD,deg mg/l Concentration of biodegradable COD

CN mg/l Concentration of total nitrogen in the homogenised sample as N

CP mg/l Concentration of phosphorus in the homogenised sample as P

CTKN mg/l Concentration of Kjeldahl nitrogen in the homogenised sample

(CTKN = CorgN + SNH4)

CorgN mg/l Concentration of organic nitrogen in the homogenised sample

(CorgN = CTKN - SNH4 or CorgN = CN - SNH4 - SNO3 - SNO2)

SALK mmol/l Alkalinity

SBOD mg/l Concentration of BOD5 in the 0.45 µm filtered sample

SCOD mg/l Concentration of COD in the 0.45 µm filtered sample

SCOD,deg mg/l Concentration of dissolved, biodegradable COD

SCOD,inert mg/l Concentration of dissolved, inert COD

SCOD,ext mg/l Concentration of dissolved COD added as external carbon for

the improvement of denitrification

SinorgN mg/l Concentration of inorganic nitrogen (SinorgN = SNH4 + SNO3 +

SNO2)

SNH4 mg/l Concentration of ammonium nitrogen in the filtered sample as N

SNO3 mg/l Concentration of nitrate nitrogen in the filtered sample as N

SNO2 mg/l Concentration of nitrite nitrogen in the filtered sample as N

SNO3,D mg/l Concentration of nitrate nitrogen to be denitrified

SNO3,D,ext mg/l Concentration of nitrate nitrogen to be denitrified with external

carbon

SNH4,N mg/l Concentration of ammonium nitrogen to be nitrified

SPO4 mg/l Concentration of phosphate as P (dissolved)

XCOD,BM mg/l Concentration of COD of the biomass

XCOD,deg mg/l Concentration of particulate, biodegradable COD

XCOD,inert mg/l Concentration of particulate, inert COD

XorgN,BM mg/l Concentration of organic nitrogen embedded in the biomass

XP,BM mg/l Concentration of phosphorus embedded in the biomass

XP,Prec mg/l Concentration of phosphorus removed by simultaneous

(11)

XP,BioP mg/l Concentration of phosphorus removed with biological excess

phosphorus removal process

XSS mg/l Concentration of suspended solids of wastewater (0.45 µm

membrane filters after drying at 105° C)

Xorg,SS mg/l Concentration of organic suspended solids of wastewater

XinorgSS mg/l Concentration of inorganic suspended solids of wastewater

Indices on the location or purpose of the sampling (always last)

I Sample from influent to the wastewater treatment plant

IAT Sample from the influent to the biological reactor, if applicable of the influent to the anaerobic mixing tank, e.g. CCOD,IAT

EAT Sample from the effluent of the biological reactor, e.g. SNO3,EAT

EDT Sample from the effluent of the denitrification tank, e.g. SNO3,EDT

ENT Sample from the effluent of the nitrification tank, e.g. SNH4, ENT

EST Sample from the effluent of the secondary settling tank, e.g. CBOD,EST, XSS,EST

WS Sample from the waste (activated) sludge RS Sample from the return (activated) sludge

ER Effluent requirement with a defined sampling procedure

3 Process Description and Procedure of Dimensioning

3.1 General

The activated sludge process is a unit process comprising the biological reactor (activated sludge tank) with the aeration equipment and the secondary settling tank, both connected by the return sludge recirculation.

The settling behaviour of the activated sludge, characterised by the sludge volume index (SVI), in combination with the mixed liquor suspended solids concentration (SSAT), influences the size of

the secondary settling tanks and biological reactors. Both the characteristics of the wastewater as well as the configuration of the biological reactor and the treatment target influence the sludge volume index. Biological reactors, which are to be considered as completely mixed tanks, usually lead to higher sludge volume indices and tend rather to the development of filamentous bacterial growth than tanks with a concentration gradient, which are such which, for example, are formed as a cascade or in which a plug flow exists. With wastewater having a high fraction of readily biodegradable organic matter, the inclusion of an upstream selector is helpful; upstream anaerobic mixing tanks for excess biological phosphorus removal do also have such a selector effect, see Fig. 1. The figure serves the nomenclature and does not imply that either an aerobic tank or a selector has to be an integral part of an activated sludge plant. However, it is pointed out that, using selectors, the growth of filamentous organisms is not controllable in all cases.

(12)

Fig.1: Flow diagram for the nomenclature of an activated sludge plant for nitrogen removal without and with an upstream anaerobic mixing tank for biological phosphorus removal or an aerobic selector

In the place of the pre-anoxic zone denitrification process shown in Fig. 1, almost all other processes for nitrogen removal and also aeration tanks, which serve only the removal of organic carbon, can be combined with an aerobic selector or an anaerobic mixing tank. The volume of an aerobic selector (VSel) or of an anaerobic mixing tank for phosphorus removal (VBioP) is

considered not to be a part of the biological reactor (VBB). In plants, which are designed only to

carbon removal, the volume of an aerobic selector can be considered as part of the aeration tank.

Relevant for the dimensioning of the biological reactor is the sludge age (tSS), which corresponds

approximately with the retention period of a sludge floc in the biological reactor. It is defined as the quotient of the mass of suspended (dry) solids in the biological reactor (VAT · SSAT) and the

daily mass of dry solids of waste activated sludge.

If the biological reactor has anoxic zones for denitrification (VD), the aerobic sludge age (tSS,aerob)

is defined as the quotient of the dry solid mass of the sludge in the aerobic part of the biological reactor (VN = VAT - VD) and the daily mass of waste activated sludge.

The residual pollution of the effluent of the secondary settling tank is, in a large part, caused by dissolved and colloidal matter and in part by suspended (activated sludge) solids. This is dependent on the efficiency of the secondary settling tank. A suspended solids concentration of 1 mg/l dry solids in the secondary settling tank effluent increases the concentration of

CBOD by 0.3 to 1.0 mg/l

CCOD by 0.8 to 1.4 mg/l

CN by 0.08 to 0.1 mg/l

(13)

3.2 Biological

Reactor

The treatment of the wastewater by the activated sludge process, with regard to process technology, operating and economic aspects, places the following requirements on the biological reactor (aeration tank):

−

sufficient enrichment of the biomass, measured simplified as the mixed liquor suspended solids concentration of the activated sludge (SSAT);

−

sufficient oxygen transfer to cover the oxygen uptake and its control to match the different operating and loading conditions;

−

sufficiently mixing in order to prevent a permanent settling of sludge on the tank bottom; as a rule ensured in aeration tanks through aeration, if required supported by mixing facilities; as guidance values for the bottom velocity in areas outside bottom installed diffused air aeration facilities, 0.15 m/s with light sludge and 0.30 m/s with heavy sludge may be assumed. In anaerobic or anoxic mixing tanks the mixing is ensured by the mixing facilities. Depending on the tank size and shape, power inputs of 1 to 5 W/m3_{are normal.}

−

no nuisances caused by odours, aerosols, noise and vibrations.

For nitrogen removal various reactor constructions and operating modes are possible (Fig. 2); these can be characterised as follows (comp. [1] 5.2.5 and 5.3.2), whereby the above listed requirements are always to be observed:

−

pre-anoxic zone denitrification process: wastewater, return sludge and internal recirculation flow are mixed in the denitrification tank. Both denitrification tanks and nitrification tanks can be formed as cascades. To increase the operating flexibility, viewed in the flow direction, the last parts of the denitrification tank can also be capable of being aerated. Internal recirculation is to be reduced to the absolutely necessary in order to minimise the negative interferences of high loads of dissolved oxygen on denitrification.

−

step-feed denitrification process: two or more biological reactors, each with pre-anoxic zone or simultaneous denitrification, are streamed one after the other. The wastewater is apportioned and fed respectively to the denitrification tanks. As a rule, through this, internal recirculation is dispensed with. High oxygen contents at the transfer from nitrification tank to the following denitrification tank prejudices the denitrification. With regard to nitrogen removal, the process is equivalent to the pre-anoxic zone denitrification process. Due to the separate feed of the wastewater, the concentration of mixed liquor in the first tank is higher than in the effluent to the secondary settling tank, comp. [1] 5.2.5.4.

−

simultaneous denitrification process: in practice only to realise in circulating flow (carousel) tanks. The circulating water flows through the denitrification and nitrification zones in the tank. One can consider simultaneous denitrification to be a type of pre-anoxic zone denitrification with a high internal recirculation ratio. An automatic control of the aeration, for example according to the nitrate content, the ammonium content, the break in the redox potential (redox break) or the oxygen content respectively the oxygen uptake rate, is necessary. With regard to the dilution, circulation tanks approximate to completely mixed tanks.

(14)

Fig. 2: Nitrogen removal procedures

−

alternating denitrification process (BioDenitro): two respectively intermittently aerated tanks are charged one after the other, whereby water flows from the charged unaerated tank into the other aerated tank and from there to the secondary settling tank. The duration of charging as well as the duration of the denitrification and the nitrification phases are, as a rule, timer controlled. High oxygen contents at the end of the nitrification phase prejudice the denitrification. The mixing behaviour lies between that of completely mixed and plug flow tanks.

−

intermittent denitrification process: the nitrification and denitrification phases alternate in time in one reactor. The duration of a phase can be timer controlled or by automatic control, for example according to the nitrate content, the ammonium content, the break in the redox potential or the oxygen uptake rate. High oxygen contents at the end of the nitrification phase prejudice the denitrification. The reactors for intermittent denitrification are to be considered as completely mixed tanks.

−

post denitrification process: the process is employed if the wastewater has a very low C/N ratio so that the addition of external carbon is unavoidable. The denitrification tank is downstream from the nitrification tank; for safety reasons a post-aeration tank follows.

(15)

[Adendum (NOT in original German text): In nitrification tanks and during nitrification phases of

intermittent processes aeration normally is automatically controlled in order to achieve a sufficient dissolved oxygen concentration (DO)].

In addition to the above-named procedures there exists a series of in part patented special processes for nitrogen removal, comp. [1], 5.2.5.

Sequencing batch activated sludge plants (SBR plants) are also suitable for nitrogen removal. Further details can be found in ATV Advisory Leaflet ATV-M 210 and in [1], 5.3.3.

A significant excess biological phosphorus removal is observed in many activated sludge plants for nitrogen removal even without an upstream anaerobic tank.

For excess biological phosphorus removal upstream of each single biological reactor or of a group of biological reactors an anaerobic mixing tank for wastewater and return sludge is placed (comp. [1], 5.2.6 and 5.3.2), Fig. 1. The effectiveness can be increased if the anaerobic tank is designed as a cascade, as then nitrate contained in the return sludge is removed in one part and in the other part completely anaerobic conditions are achieved. Attention is drawn to [1], 5.2.6 for special procedures. Facilities for simultaneous phosphorus precipitation are provided in most plants with excess biological phosphorus removal. The precipitant dosing should as far as possible be automatically controlled whereby a control system in the outflow of the aeration tank is preferred.

Excess biological phosphorus removal is also possible in activated sludge plants which are designed only for carbon elimination, if the sludge age tSS is at least 2 to 3 days.

3.3 Secondary Settling Tank

Secondary settling tanks have the main task of separating the activated sludge from the biologically treated wastewater .

The loading capacity of an activated sludge plant is determined substantially by the concentration of suspended solids (SSAT) of the activated sludge and the volume of the aeration tank. The

concentration of suspended solids depends essentially on the functional capability of the secondary settling tanks with fluctuating hydraulic feeding, the sludge volume index and the sludge removal as well as the return sludge ratio and the waste sludge removal.

Dimensioning, design and equipping of secondary settling tanks must be carried out that the following tasks can be met:

−

separation of the activated sludge from treated wastewater by settling;

−

thickening and removal of the settled activated sludge for recirculation to the biological reactor (aeration tank);

−

intermediate storage of activated sludge which, as a result of increased inflow rates at stormwater periods (QWW,h), is expelled from the aeration tank.

The settling process in the secondary settling tank is influenced by the flocculation process in the inlet zone, the hydraulic conditions in the secondary settling tank (design of the inlet and outlet, density currents) the return sludge ratio and the sludge removal procedure. The settled sludge is concentrated in the sludge layer on the tank bottom. The thickening achieved therein is dependent on the sludge properties (SVI), the depth of the sludge layer, the thickening time and the type of the sludge removal system.

With stormwater inflow activated sludge is relocated increasingly from the aeration tank into the secondary settling tank. The secondary settling tank must then be able to store the sludge

(16)

expelled from the aeration tank. For this a sufficiently large storage volume, an efficient sludge removal system and appropriately dimensioned sludge return facilities (e.g. pumps) are required. With regard to the method of function one differentiates between horizontal and vertical flow secondary settling tanks. Circular and rectangular tanks are differentiated according to design. The settled and thickened sludge, so far as it does not flow automatically into the sludge hopper, is transported by blade or flight scrapers or is removed directly using suction facilities.

3.4 Procedure of Dimensioning

The dimensioning of activated sludge plants takes place iteratively, as many factors influence each other mutually, comp. Fig. 3. The calculation path given below practically represents one calculation run after which it can be necessary to repeat the calculations with new assumptions.

(17)

The following steps are recommended:

1 determination of the dimensioning capacity of the plant and the relevant flows and loads to the biological reactor, comp. Chap. 4.

2 selection of the process: if nitrogen removal is required, it has to be decided which process for nitrification/denitrification is to be employed. In addition it is to be determined whether an aerobic selector for the improvement of the settling characteristics or an anaerobic mixing tank for biological excess phosphorus removal is to be placed upstream.

3 determination of the necessary safety factor (SF) taking into account the dimensioning capacity of the plant and, in case, the measured diurnal load fluctuations. For plants which are designed for nitrification only, the sludge age (tSS,aerob,dim) is to be determined taking into

account the dimensioning temperature. Both are omitted with aerobic sludge stabilisation. 4 with plants for nitrogen removal the mass of the nitrate to be denitrified is to be determined

by means of a nitrogen balance. If not a percentage of nitrogen removal is to be maintained but rather a concentration value, the influent concentration is of great influence; if the concentration in a random sample is to be met (e.g. qualified random sample in accordance with the Wastewater Ordinance in Germany), this must be taken specially into account with the dimensioning.

5 taking into account the selected denitrification process the necessary proportion of the denitrification volume to the biological reactor volume (VD/VAT) is to be determined. The

sludge age (tSS,dim) is to be calculated accordingly. For combined aerobic sludge stabilisation

the sludge age is to be selected, if appropriate in accordance with the relevant wastewater temperature.

6 selection of the sludge volume index taking into account the composition of the wastewater, the configuration and the mixing characteristics of the biological reactor as well as, if selected, an aerobic selector or anaerobic mixing tank.

7 selection of the sludge thickening time (tTh) in the secondary settling tank dependent on the

biological process selected and determination of the concentration of (dry) suspended solids in the bottom sludge (SSBS) as function of SVI and tTh.

8 determination of the return sludge suspended solids concentration (SSRS) from the

achievable concentration of suspended solids in the bottom sludge and the dilution of the sludge removal stream dependent on the selected sludge removal system.

9 selection of the return sludge ratio (RS) and estimation of the permissible suspended solids concentration of the activated sludge in the biological reactor (SSAT).

The mixed liquor suspended solids concentration of the activated sludge influences the volumes of biological reactors and secondary settling tanks in the opposite sense. It is to be noted that the volume of the biological reactor reduces with increasing SSAT while, with

increasing SSAT, the surface area of the secondary settling tanks and, in addition, the depth

become greater.

10 determination of the surface area of the secondary settling tank (AST) from the permissible

surface overflow rate (qA) or the sludge volume loading rate (qSV).

11 determination of the depth of the secondary settling tank from partial depths for the functional zones and other specifications.

12 verification of the selected thickening time by the sludge removal (scraper) performance, prerequisite is that the dimensions of the secondary settling tank are laid down.

(18)

13 determination of the waste sludge production (SPd), if required taking into account waste

sludge from phosphorus removal and the possibly dosed external carbon for denitrification. 14 calculation of the required mass of solids in the biological rector (MSS,AT) for the selected

sludge age.

15 calculation of the volume of the biological reactor.

16 if required, dimensioning of an anaerobic mixing tank for biological phosphorus removal. 17 calculation of the necessary internal recirculation flow rate for pre-anoxic zone denitrification

or the cycle time with intermittent denitrification processes.

18 determination of the relevant oxygen consumption for the design of the aeration facility. 19 checking of the remaining alkalinity and/or the necessity for dosing lye taking into account

consumption and gain in alkalinity from ammonification, nitrification, denitrification and phosphate precipitation as well as the oxygen utilisation and diffuser depth (The latter only to determine the pH in the biological reactor).

20 if required, dimensioning of an aerobic selector for the improvement of the settling properties of the activated sludge.

The dimensioning parameters can be laid down on the basis of scientific model concepts and supported by experience or, in part, can be derived from experiments carried out on site.

4 Dimensioning Flows and Loads

4.1 Loading with Wastewater

The dimensioning value of the wastewater treatment plant Bd,BOD,I in kg/d BOD5 (raw) for the

classification into the Size Class in accordance with Appendix 1 to the [German] Wastewater Ordinance and for the determination of the dimensioning capacity of the plant in the Assessment under Water Law is derived from the BOD5 load in the influent to the wastewater treatment plant

which is undercut on 85 % of the dry weather days, plus a planned capacity reserve. If the dimensioning capacity is determined based on the number of connected inhabitants, the inhabitant-specific BOD5 load for raw wastewater from Table 1 is to be used.

In principle it applies that sewer system and sewage treatment plant are to be operated for the same wastewater effluent and influent.

For the dimensioning, the following important numerical values are required from the influent to the biological reactor, if applicable with the inclusion of the return flows from sludge treatment (comp. 4.2):

−

relevant lowest and highest wastewater temperature. Determination from the curve of the 2-week mean over two to three years.

−

relevant organic load (Bd,BOD Bd,COD), the relevant load of suspended solids (Bd,SS) and of

phosphorus (Bd,P) for the determination of the sludge production and thus the calculation of

(19)

−

relevant organic load and nitrogen load for the design of the aeration facility for (as a rule) the highest relevant temperature.

−

relevant concentration of nitrogen (CN) and the related concentration of organic substances

(CBOD, CCOD) for the determination of the nitrate to be denitrified.

−

relevant concentration of phosphorus (CP) for the determination of the phosphorus to be

removed.

−

maximum inflow rate with dry weather QDW,h (m3/h) for the design of the anaerobic mixing

tank and the internal recirculation flow rate.

−

dimensioning inflow rate QWW,h (m3/h) for the design of the secondary settling tanks.

Daily loads can only be calculated on the basis of volumetric- or flow proportional 24 hr composite samples and the related daily inflow. The relevant loads are to be determined on the basis of measurements on arbitrary days, i.e. with the inclusion of wet weather days.

If an annual graph indicates periodical fluctuations of the organic loads or/and the ratio of organic load to nitrogen load, several loading cases are to be investigated.

The relevant concentrations are to be determined using the relevant loads and the associated daily wastewater inflows. The relevant loads for periods with relevant wastewater temperatures, are made up as mean value of a period of time, which corresponds with the sludge age. Simplified for nitrification and denitrification two-week means and, for sludge stabilisation, four-week means can be made up. If, in the absence of sufficient sampling density (at least four utilisable daily loads per week), weekly means cannot be made up, then the loads which are undercut on 85 % of the days are relevant, whereby at least 40 load values should be used. If the data are insufficient or the expense of investigations, for example with small plants, are in no relation to the use, loads and concentrations can be determined on the basis of connected inhabitants plus industrial-commercial and other loads.

Details on the determination of the relevant loads and concentrations are to be found in the Standard ATV-DVWK-A 198 [in preparation] "Unification and derivation of dimensioning values for wastewater systems" [3].

If the relevant loads have to be estimated using the connected inhabitants, the values in Table 1 can be used. The estimate of the associated wastewater inflow is to be undertaken in accordance with the ATV-DVWK Standard [3]. Until publication of that Standard the determination of the wastewater inflow can be undertaken in accordance with ATV Standard ATV-A 131 (1991) [not translated into English].

Table 1: Inhabitant-specific loads in g/(I·d), which are undercut on 85 % of the days, without taking into account sludge liquor

Flow time in the primary settling stage with Qh,DW

Parameter Raw wastewater

0.5 to 1.0 h 1.5 to 2.0 h BOD5 60 45 40 COD 120 90 80 DS 70 35 25 TKN 11 10 10 P 1.8 1.6 1.6

(20)

Deliberate wastewater investigations and determinations of loads over two to four weeks cannot, as a rule, be used directly for dimensioning as one cannot be sure of having recorded the relevant time period. They are, however, practical for the supplementing of the existing database. With such investigations the inflows associated with the sampling intervals are always to be recorded. Thus the diurnal TKN curves for the determination of the fN value (comp. 5.2.8) can be

recorded. Seldom analysed values such as, for example, the suspended solids concentration (XSS,IAT) or the alkalinity (SALK,IAT) can thus be covered. The loading of internal return flows e.g.

from sludge treatment should also be recorded within the scope of such investigations.

4.2 Loading with Sludge Liquor and External Sludge

Water from the thickening and dewatering of (anaerobic) digested sludge contains ammonium in high concentrations. It can be assumed that 50 % of the organic nitrogen introduced into the sludge digester is released as ammonium nitrogen. If sludge liquor is produced for a few hours daily only or only on odd days weekly, an intermediate storage for dosed input is necessary. The return loading with phosphorus and organic matter (BOD5 and COD) is, as a rule, small from

dewatering of digested sludge. Therefore a return loading may not be added, for example, globally as a percentage to all loads from the wastewater.

In sludge silos for aerobic stabilised sludge, as a rule, more or less anaerobic processes occur. With this, ammonium can be released and redissolution of phosphorus is possible, if excess biological phosphorus removal is applied. In order to minimise impairment of the biological treatment

−

sludge liquor should be drawn off regularly in small quantities

−

when dewatering the silo content filtrate or centrate should be collected in silos of a similar size and be fed to the inlet over a long period of time.

If external sludge (sludge from other sewage treatment plants, faecal sludge or similar) is discharged then an intermediate storage can be sensible, in order to make a dosed input possible.

5 Dimensioning of the Biological Reactor

5.1 Dimensioning on the Basis of Pilot Experiments

Pilot testing using pilot plants or a part of the full size plant serve for the examination of a process concept and of the model parameters under practice-oriented conditions.

The pilot plants for this are to be established at least on a semi-technical scale and are to be operated under practice-oriented operating conditions for not shorter than half a year with the inclusion of the cold season. One can carry out a weakest-point analysis beforehand with the aid of dynamic simulation. From this one can gather valuable information for planning of the test runs.

Through such investigations the dimensioning is, as a rule, more correct and often costs can be saved. Using the results an improved basis for the dynamic simulation of operational conditions not recorded during the experiments is then also created.

(21)

Some of the dimensioning parameters given under Sect. 3.4 can be determined with

this, these are, for example:

−

the sludge production and the necessary sludge age.

−

the practical subdivision of the biological reactor (anaerobic, anoxic and aerobic), if required for the various seasons and/or loading conditions.

−

the oxygen consumption and the requirements for automatic control of the oxygen transfer; for this the oxygen uptake rate has to be measured frequently.

−

the dissolved residual COD (SCOD,EST)

5.2 Dimensioning on the Basis of Experience

5.2.1 Required Sludge Age

5.2.1.1 Plants without Nitrification

Activated sludge plants without nitrification are dimensioned for sludge ages of four to five days, comp. Table 2.

Table 2: Dimensioning sludge age in days dependent on the treatment target and the temperature as well as the plant size (intermediate values are to be estimated)

Size of the plant Bd,BOD,I

Treatment target Up to 1,200 kg/d Over 6,000 kg/d Dimensioning temperature 10° C 12° C 10° C 12° C

Without nitrification 5 4

With nitrification 10 8.2 8 6.6

With nitrogen removal VD/VAT = 0.2 0.3 0.4 0.5 12.5 14.3 16.7 20.0 10.3 11.7 13.7 16.4 10.0 11.4 13.3 16.0 8.3 9.4 11.0 13.2 Sludge stabilisation incl. nitrogen

(22)

5.2.1.2 Plants with Nitrification

The (aerobic) dimensioning sludge age to be maintained for nitrification is:

) 15 ( dim , ,aerob

3 .

4

1 .

103

T SS

SF

t

=

⋅

−

[d]

(5-1)

The value of 3.4 is made up from the reciprocal of the maximum (net) growth rate of the ammonium oxidants (nitrosomonas) at 15° C (2.13 d) and a factor of 1.6. Through the latter it is ensured that, with sufficient oxygen transfer and no other negative influence factors, enough nitrificants can be developed or held in the activated sludge, (comp. [1] 5.2.4). With a sludge age of 2.13 d (15° C), nitrificants cannot accumulate.

Using the safety factor (SF) the following are taken into account:

−

variations of the maximum growth rate caused by certain substances in the wastewater, short-term temperature variations or/and pH shifts.

−

the mean effluent concentration of the ammonium.

−

the effect of variations of the influent nitrogen loads on the variations of the effluent ammonia concentration.

Based on all previous experience it is recommended, for municipal plants with a dimensioning capacity up to Bd,BOD,I = 1,200 kg/d (20,000 PT), to reckon with SF = 1.8 due to the more

pronounced influent load fluctuation and for Bd,BOD,I ≥ 6,000 kg/d (100,000 PT) with SF = 1.45.

With this, the effluent concentration on average, can be held at SNH4,EST = 1.0 mg/l, so long as no

negative influencing of the maximum growth rate of the nitrificants exists.

If, with plants with Bd,BOD,I < 6,000 kg/d, the measured fN value lies below 1.8 (comp. 5.2.8), SF

can be reduced down to 1.45.

If a buffering tank for daily balancing of the load is planned the safety factor shall not be assumed smaller than SF = 1.45.

If, in winter, the temperature in the outflow of the biological reactor sinks below the temperature at which the effluent requirement for ammonium has to be held (TER), the dimensioning value in

Eqn. 5-1 Tdim = (TER - 2) is to be applied, in order to achieve a stable nitrification at the control

temperature. It is proposed that, for the control temperature of TER = 12° C in dependence on the

size of the plant taking into account the above-given safety factor to select the following dimensioning sludge ages:

Plants up to Bd,BOD,I = 1,200 kg/d

tSS,aerob,dim = 10 d

Plants above Bd,BOD,I = 6,000 kg/d

tSS,aerob,dim = 8 d

These values are given in Table 2. Intermediate values are to be interpolated.

If the wastewater temperature is always higher than the control temperature, the lowest two-week mean of the temperature can be selected as the dimensioning temperature.

In order to limit the heavy consumption of alkalinity (comp. 5.2.9) through nitrification, it is recommended, for operational reasons, to plan a partial denitrification, comp. 5.2.1.3.

(23)

5.2.1.3 Plants with Nitrification and Denitrification

Prerequisite for nitrogen elimination is a secure nitrification, comp. 5.2.1.2.

For nitrification and denitrification the dimensioning sludge age results as follows:

)

/

(

1

, dim , AT D aerob SS SS

V

t

−

⋅

=

[d] (5-2) With Eqn. 5-1:

)

/

(

1

103 .

1

4 .

3

(15 ) dim , , AT D T aerob SS

V

SF

t

−

⋅

=

− [d] (5-3)

Attention is drawn to Sect. 5.2.2 for the calculation of VD/VAT.

In Eqn. 5-3 the temperature to be applied as dimensioning temperature is that at which nitrogen elimination is required (Tdim = TER); thus, in accordance with the Wastewater Ordinance in

Germany, Tdim = TER = 12° C.

For the wastewater temperatures which, as a rule, in winter are lower than 12° C, proof is to be furnished that, with the lowest two-week mean of the temperature, the nitrification does not break down. For this, maintaining the dimensioning sludge age, the portion VD/VAT for the lower

temperature (TW) is calculated according to Eqn. 5-4.

If there are no acceptable measured values available for the wastewater temperature, the temperature tER, reduced by 2° to 4° C, should be applied in Eqn. 5-4 for TW. (2 C, if a cooling of

the wastewater below 10° C in the two-week mean is not to be expected and 4° C, if in extreme situations heavier cooling is to be reckoned with).

If, with the lower temperatures, the organic loading (Bd,BOD,I) is an other than the one on which

dimensioning is based, the actual sludge age should be applied in Eqn. 5-4 instead of tSS,dim.

dim , ) 15 (

103 .

1

4 .

3 /

SS T AT D

V

SF

_t

V

=

⋅

− W [-] (5-4)

This proof assumes a flexible design of the biological reactor, whereby the denitrification zone has to be reducible in favour of the nitrification zone. A possibly available anaerobic mixing tank can be included in the volume VD at pre-anoxic zone denitrification, if the internal recirculation is

appropriately designed.

If, according to Eqn. 5-4, there is a negative value for VD/VAT, then VD/VAT = 0 is applied and the

safety factor is to be calculated using Eqn. 5-4. It can be lowered down to SF = 1.2; otherwise the reactor volume is to be increased.

Should a dimensioning temperature below 12° C be required, one proceeds accordingly. There is no experience available about the dimensioning of plants for a temperature below 8° C.

In every case it is to be verified whether the remaining alkalinity is sufficient, comp. Sect. 5.2.9. If the effluent requirement for ammonium nitrogen is set with SNH4,ER < 10 mg/l or the influent

loads are subject to very high variations, even in dry weather, and the monitoring takes place on a random sample or a 2 h composite sample, the safety factor is to be increased or a verification

(24)

with the aid of dynamic simulation is be carried out. This calls for the measurement of the appropriate diurnal load fluctuations.

5.2.1.4 Plants with Aerobic Sludge Stabilisation

The dimensioning sludge age of plants, which are to be dimensioned for aerobic sludge (co-) stabilisation and nitrification, must be tSS,dim ≥ 20 d.

If deliberate denitrification is also required the sludge age must be tSS,dim ≥ 25 d. If the

temperature in the biological reactor in the two-week mean is always higher than 12° C, the sludge age can be reduced in accordance with Eqn. 5-5.

) 12 ( dim ,

25

1 .

072

T SS

t

≥

⋅

− [d] (5-5)

If the organic loads in the warm season are higher than those in the cold season, the required mass of sludge MSS,AT (comp. 5.2.6) have to be determined separately for both cases using Eqn.

5.5. The greater mass of sludge is relevant for the biological reactor volume.

If sludge ponds or tanks with at least a storage duration of one year of the liquid sludge for anaerobic post-stabilisation are available, the sludge age, even if deliberate denitrification is demanded, can be lowered to tSS,dim = 20 d.

The calculation of the nitrate to be denitrified and the volume fraction VD/VAT takes place

according to Sect. 5.2.2. VD/VAT has no influence on the sludge age but rather serves, for

example with intermittent denitrification, for the calculation of the oxygen transfer.

5.2.2 Determination of the Proportion of the Reactor Volume for Denitrification

The daily average nitrate concentration to be denitrified results as follows:

BM orgN EST NO EST NH EST orgN IAT N D NO

C

S

X

S

₃_,

=

_,

−

_,

−

₄_,

−

₃_,

−

_, [mg/l] (5-6) As influent nitrogen concentration (CN,IAT) the relevant value determined for T = 12° C is to be

applied. If, during the year, at the times of higher temperatures, higher CN,IAT/CCOD,IAT ratios have

been determined, in case several types of load are to be considered.

The influent nitrate concentration (SNO3,IAT) is, in general, negligibly small. With greater infiltration

rates (groundwater containing nitrate) or with inflows from certain commercial and industrial plants, it can be necessary to take account of SNO3,IAT in CN,IAT.

At plants with anaerobic sludge digestion and mechanical dewatering at the site, the nitrogen of the sludge liquor must be contained in the inflow concentration (CN,IAT) if no separate sludge

liquor treatment takes place, comp. Sect. 4.2. The concentration of organic nitrogen in the effluent can be set as SorgN,EST = 2 mg/l. With the inflow of certain commercial wastewater the

concentration can be higher. To be on the safe side the ammonium content in the effluent for dimensioning is, as a rule, assumed as SNH4,EST = 0. The nitrogen incorporated in the biomass is

taken into account simplified as XorgN,BM = 0.04 to 0.05·CBOD,IAT or 0.02 to 0.025·CBOD,IAT.

The relevant effluent concentration of the nitrate is to be applied as daily average, If, as in Germany, the monitoring takes place by means of random grab or 2 hour composite samples, a significantly smaller concentration than the effluent requirement for inorganic nitrogen (SinorgN,ER)

has to be selected. It is practical to set SNO3,EST = 0.8 to 0.6·SinorgN,ER, whereby the smaller value

(25)

With the relevant BOD5 of the inflow to the biological reactor (or to the anaerobic mixing tank)

one obtains the ratio SNO3,D/CBOD,IAT, which gives the necessary denitrification capacity.

For simultaneous and intermittent denitrification processes the following calculation of VD/VAT can

be applied, comp. [1], 5.2.5.3: AT D BOD C IAT BOD D NO

V

OU

C

S

⋅

=

9 .

2

75 .

0

_, , , 3 _{[mg N/mg BOD} 5] (5-7)

[Addendum (NOT in original German text): Eqn. 5-7 is derived from a mass balance of oxygen in the denitrification zone of a completely mixed biological reactor.]

AT C d D D NO d

V

OU

V

S

Q

₃_, _,

75 .

0 1000

9 .

2 ⋅

⋅

=

⋅

[kg/d]

The left hand side represents the oxygen provided by the daily nitrate load to be denitrified. The right side shows the daily uptake of oxygen in the denitrification zone. The factor 0.75 indicates an overall lower uptake rate of nitrate compared to the uptake rate of dissolved oxygen].

OUC,BOD is to be determined in accordance with Eqn. 5-24 for the dimensioning sludge age and

the dimensioning temperature or is to be taken from Table 7. For the temperature range from 10° to 12° C the values calculated using Eqn. 5-7 are listed in Table 3.

For pre-anoxic zone denitrification process and comparable processes, at which only a small part of the readily biodegradable organic matter is lost for the denitrification, the empirical values listed in Table 3, which match the tendency towards the theoretically derivable values, apply, comp. [1], Fig. 5.2.5-3. Prerequisite is that in all influents to the denitrification zone the dissolved oxygen content is kept at less than 2 mg/l.

Table 3: Standard values for the dimensioning of denitrification for dry weather at temperatures from 10° to 12° C and common conditions (kg nitrate nitrogen to be denitrified per kg influent BOD5)

SNO3,D/CBOD,IAT

VD/VAT Pre-anoxic zone denitrification

and comparable processes Simultaneous and intermittent denitrification

0.2 0.11 0.06 0.3 0.13 0.09 0.4 0.14 0.12 0.5 0.15 0.15

For the temperature range from 10° to 12° C it is recommended to use for dimensioning the values for the denitrification capacity in Table 3. Denitrification volumes smaller than VD/VAT = 0.2

and greater than VD/VAT = 0.5 are not recommended for dimensioning.

The denitrification capacity with the alternating denitrification process can be assumed to be the average between pre-anoxic zone and intermittent denitrification.

(26)

For temperatures above 12° C the denitrification capacity can be increased by ca. 1 % per 1° C. If the dimensioning or re-calculation takes place on the basis of COD, one can reckon with SNO3,D/CCOD,IAT = 0.5·(SNO3,D/CBOD,IAT.).

With re-calculation for a value of VD/VAT = 0.1, one can reckon with SNO3,D/CBOD,IAT = 0.08 for

pre-anoxic zone denitrification and SNO3,D/CBOD,IAT = 0.03 for simultaneous and intermittent

denitrification. If, by re-calculation a value of VD/VAT < 0.1 is obtained then SNO3,D/CBOD,IAT = 0 is to

be set.

If the required denitrification capacity is larger than SNO3,D/CBOD = 0.15, then a further increase of

VD/VAT is not recommended. It is to be investigated whether a volume reduction or partial

by-passing of the primary settling tank and/or, if applicable, a separate sludge treatment are conducive to meeting the target. An alternative is to carry out the planning for the addition of external carbon. The construction of the appropriate facilities should, however, first be undertaken, if secured operational experience is available.

The requirement for external carbon is ca. 5 kg COD per kg of nitrate nitrogen to be denitrified. With this one obtains the average increase of the COD as:

Ext D NO Ext COD

S

_,

=

5 ⋅

₃_, _, [mg/l] (5-8) The COD of commercial carbon compounds can be taken from Table 4. For other sources of carbon the COD and, if necessary, the denitrification capacity, are to be determined in advance. It is pointed out that methanol is only suitable for a long-term application as special denitrificants have to be grown.

Table 4: Characteristics of external carbon sources

Parameter Unit Methanol Ethanol Acetic acid

Density kg/m3_{790 780 1,060}

COD kg/kg 1.50 2.09 1.07

COD kg/L 1.185 1.630 1.135

5.2.3 Phosphorus

Removal

Phosphorus removal can take place alone through simultaneous precipitation, through excess biological phosphorus removal, as a rule combined with simultaneous precipitation, and through pre- or post precipitation (comp. [1], 5.2.6 and 7.4).

Anaerobic mixing tanks for biological phosphorus removal are to be dimensioned for a minimum contact time of 0.5 to 0.75 hours, referred to the maximum dry weather inflow and the return sludge flow (QDW,h + QRS). The degree of the biological phosphorus removal depends, other than

on the contact time, to a large extent on the ratio of the concentration of readily biodegradable organic matter to the concentration of phosphorus. If, in winter, the anaerobic volume is used for denitrification, then during this period a lower biological excess phosphorus removal will establish.

For the determination of the phosphate to be precipitated a phosphorus balance, if necessary for different types of load, is to be drawn up:

(27)

BioP P BM P EST P IAT P P

C

X

_,_Prec

=

_,

−

_,

−

_,

−

_, [mg/l] (5-9) CP,IAT is the concentration of the total phosphorus in the influent to the biological reactor. The

effluent concentration (CP,EST) is to be selected in agreement with the effluent requirement for

phosphorus (CP,ER), e.g. CP,EST = 0.6 to 0.7 CP,ER. The phosphorus necessary for the build-up

heterotrophic biomass (XP,BM) can be set as 0.01 CBOD,IAT or 0.005 CCOD,IAT respectively. With

normal municipal wastewater one can assume the following for the excess biological phosphorus removal (XP,BioP):

−

XP,BioP = 0.01 to 0.015 · CBOD,IAT or 0.005 to 0.007 CCOD,IAT respectively with upstream

anaerobic tanks.

−

if, with lower temperatures, SNO3,EST increases to ≥ 15 mg/l, it can be assumed: XP,BioP = 0.005

to 0.01 CBOD,IAT or 0.0025 to 0.005 · CCOD,IAT respectively with upstream anaerobic tanks.

−

in plants with pre-anoxic zone denitrification or step-feed denitrification, but without anaerobic tanks, an excess biological phosphorus removal of XP,BioP ≤ 0.005 CBOD,IAT or 0.002 CCOD,IAT

respectively can be assumed.

−

if, at low temperatures, the internal recirculation of pre-anoxic zone denitrification is discharged into the anaerobic tank, one can reckon with XP,BioP ≤ 0.005 CBOD,IAT or 0.002

CCOD,IAT respectively.

The mean precipitant requirement can be calculated using 1.5 mol Me3+_{/mol X}

P,Prec. Converted

the following requirement values are obtained:

Precipitation using iron 2.7 kg Fe/kg PPrec

Precipitation using aluminium 1.3 kg Al/kg PPrec

For simultaneous precipitation using lime, as a rule, milk of lime is dosed into the influent to the secondary settling tank in order to raise the pH and through this to bring about precipitation. In the first instance, the requirement for lime depends on the alkalinity. Tests are in any case recommended, comp. ATV Standard ATV-A 202 [not yet available in English].

For control values of CP,ER < 1.0 mg/l, e.g. CP,ER = 0.8 mg/l in the qualified random sample,

single-stage activated sludge plants cannot be dimensioned. In practice, however, values of CP,EST = < 1.0 mg/l can be achieved under favourable conditions.

5.2.4 Determination of the Sludge Production

The sludge produced in an activated sludge plant is made up of organic matter resulting from degradation and stored solid matter as well as sludge resulting from phosphorus removal:

P d C d d

SP

=

_,

+

_, [kg/d] (5-10)

The relationship of sludge production and sludge age can be written as follows:

EST SS d WS d WS AT AT d AT AT d AT SS SS

X

Q

SS

Q

SS

V

SP

SS

V

SP

M

t

, , ,

⋅

+

⋅

=

⋅

=

[d] (5-11)

As the load of filterable matter in the effluent of the secondary settling tank (Qd·XSS,EST) is, as a

rule, negligible, the sludge production (SPd) can be assumed to be the same as the daily waste

(28)

For the calculation of the sludge production from carbon removal the following empirical equation using the Hartwig coefficients can be used (comp. [1], 5.2.8.2):

)

17 .

0

1

75 .

0

17 .

0 )

2 .

0

1 (

6 .

0

75 .

0 (

, , , , T SS T SS IAT BOD IAT SS BOD d C d

F

t

F

t

C

X

B

SP

⋅

+

⋅

−

⋅

+

⋅

=

[kg/d] (5-12)

The temperature factor (FT) for the endogenous respiration is: ) 15 T ( T

1 .

072 F

₌

− _[-] _(5-13)

If external carbon has to be dosed regularly for the improvement of denitrification, then with SCOD,Ext ≥ 10 mg/l (SNO3,D,Ext ≥ 2 mg/l) simplified in Eqn. 5-12, Bd,BOD is to be increased by the

value Qd·0.5·SCOD,Ext/1000 and in Eqn. 5-12 as well as in Table 5 CBOD,IAT by the value 0.5·SCOD,Ext.

With SCOD,Ext ≤ 10 mg/l the additional sludge production is ignored.

The values in Table 5 are calculated and averaged using Eqn. 5-12 for T = 10° C and 12° C.

Table 5: Specific sludge production SPC,BOD [kg SS/kg BOD5] at 10° to 12° C

Sludge age in days XSS,IAT/ CBOD,IAT 4 8 10 15 20 25 0.4 0.79 0.69 0.65 0.59 0.56 0.53 0.6 0.91 0.81 0.77 0.71 0.68 0.65 0.8 1.03 0.93 0.89 0.83 0.80 0.77 1.0 1.15 1.05 1.01 0.95 0.92 0.89 1.2 1.27 1.17 1.13 1.07 1.04 1.01 The sludge production from the phosphorus removal is made up of the solid matter from the excess biological phosphorus removal and that from simultaneous precipitation.

For the excess biological phosphorus removal one can reckon with 3 g SS per g biologically removed phosphorus. The solids yield from simultaneous precipitation is dependent on the type of precipitant and the amount of dosing, comp. Sect. 5.2.3. One should reckon with a sludge production of 2.5 kg SS per kg dosed iron and 4 kg SS per kg dosed aluminium. The total sludge production resulting from phosphorus removal (SPd,P) thus results as follows:

1000

/

)

3 .

5

8 .

6

3 (

_, _, _, _, _,

,P d PBioP PPrecFe PPrecAl

d

Q

X

SP

=

⋅

+

⋅

+

⋅

[kg/d] (5-14)

If lime is used for precipitation the sludge production is 1.35 kg SS per kg calcium hydroxide (Ca(OH)2); see also ATV Standard ATV-A 202.

5.2.5 Assumption of the Sludge Volume Index and the Mixed Liquor Suspended

Solids Concentration

The sludge volume index depends on the composition of the wastewater and the mixing characteristics of the aeration tank. A high fraction of readily biodegradable organic matter, as are contained in some commercial and industrial wastewater, can lead tohigher sludge volume indices.

atv-dvwk_a_131_e

GERMAN ATV-DVWK

RULES AND STANDARDS

STANDARD

ATV-DVWK-A 131E

Dimensioning of Single-Stage Activated Sludge Plants

May 2000

ISBN 3-935669-96-8

Preparation

Contents

Notes for Users

Foreword

•

•

•

•

•

•

•

•

•

•

•

1 Area

of

Application

1.1 Preamble

1.2 Objective

1.3 Scope

2 Symbols

V

m

Volume of an aerobic selector

V

m

Volume of the secondary settling tank

v

m/h

Return velocity of the scraper bridge

v

m/h

Scraper bridge velocity (with circular tanks at the

periphery)

3

Process Description and Procedure of Dimensioning

3.1 General

3.2 Biological

Reactor

−

−

−

−

−

−

−

−

−

−

3.3

Secondary Settling Tank

−

−

−

3.4

Procedure of Dimensioning

4

Dimensioning Flows and Loads

4.1

Loading with Wastewater

−

−

−

−

−

−

−

4.2

Loading with Sludge Liquor and External Sludge

−

−